CN109851581B - Method for purifying butylene oxide - Google Patents
Method for purifying butylene oxide Download PDFInfo
- Publication number
- CN109851581B CN109851581B CN201810153545.4A CN201810153545A CN109851581B CN 109851581 B CN109851581 B CN 109851581B CN 201810153545 A CN201810153545 A CN 201810153545A CN 109851581 B CN109851581 B CN 109851581B
- Authority
- CN
- China
- Prior art keywords
- extractant
- butanediol
- dimethyl ether
- butylene oxide
- azeotrope
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Active
Links
Images
Landscapes
- Epoxy Compounds (AREA)
Abstract
The invention relates to a method for purifying butylene oxide, which mainly solves the problems of low purity, large loss, low yield of propylene oxide and high energy consumption of an extracting agent caused by accumulation of impurities of heavy components of butanediol monomethyl ether and butanediol dimethyl ether in the prior art. The method comprises the steps of separating a feed stream containing butylene oxide, an extractant and butanediol monomethyl ether and butanediol dimethyl ether in a separation column; the separation column is operated under conditions sufficient for the extractant to form an azeotrope with butanediol monomethyl ether and butanediol dimethyl ether, and a stream containing the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope is taken off at the side of the separation column. The method can be used in the industrial production of butylene oxide.
Description
Technical Field
The invention relates to a production method of epoxy butane, in particular to a purification method for extracting, rectifying and recovering an extracting agent from epoxy butane.
Background
1, 2-Butylene Oxide (BO) and Ethylene Oxide (EO) and Propylene Oxide (PO) belong to homologues with a molecular formula of C4H8O (CAS number: 106-88-7), are substances with a ternary ring structure, are chemically active and are mainly used as polyether polyol monomers and intermediates of other synthetic materials. The epoxy butane can also be used for preparing foam plastics, synthetic rubber, nonionic surfactants and the like, can also replace acetone to be used as a diluent of nitrolacquer, and can also be used as a standard substance for chromatographic analysis.
As the olefin epoxide, compared with ethylene oxide and propylene oxide, the molecular structure of the epoxy butane has a larger amount of-CH 2-functional groups, and when the molecular structure of the epoxy butane is used as a monomer to synthesize polyether polyol, the product has excellent hydrophobic property, and is particularly suitable for the outer surface waterproof coating of certain buildings and equipment with strict requirements. Meanwhile, the polyurethane material synthesized by copolymerization with the butylene oxide as a monomer has excellent cold resistance, and is particularly suitable for cold climate areas.
The butylene oxide product has strict requirements on water, aldehyde and isomers, the water can influence the hydroxyl value and the foaming performance of the polymer, the aldehyde content is an environment-friendly requirement, and the isomers are end capping agents of long polymer chains, so that the product purity is strictly required in national standards and enterprise standards.
The quality and purity requirements of the qualified 1, 2-butylene oxide product in BASF enterprise standards are as follows: more than or equal to 99.5 percent of butylene oxide, less than or equal to 0.2 percent of butylene oxide isomer, less than or equal to 0.05 percent of total aldehyde and less than or equal to 0.03 percent of water.
The quality and purity requirements of the 1, 2-epoxybutane superior products are as follows: more than or equal to 99.9 percent of butylene oxide, less than or equal to 0.1 percent of butylene oxide isomer, less than or equal to 0.015 percent of total aldehyde and less than or equal to 0.005 percent of water.
The crude butylene oxide generated by the reaction usually contains impurities such as water, acetaldehyde, methanol, acetone, methyl formate and the like, and because the impurities and the butylene oxide form an azeotrope or the relative volatility is close to 1, the common rectification can not reach the standards of the butylene oxide product. In order to obtain high-purity butylene oxide satisfying the polymerization requirements, it is necessary to separate and remove impurities contained in butylene oxide. The purification of butylene oxide generally adopts C7-C20 straight-chain and branched-chain hydrocarbons and (or) glycols as an extracting agent. For economic reasons, mixtures of C8 linear and branched alkanes were used as extractants. The addition of the extractant increases the relative volatility of acetaldehyde, water, methanol and methyl formate to epoxybutane, and the acetaldehyde, water, methanol and methyl formate are removed from the top of the tower.
The butene epoxidation reaction product mainly contains 1, 2-epoxybutane and isomers thereof such as 1, 4-epoxybutane, 2, 3-epoxybutane and epoxyisobutane. In the process of refining the butylene oxide, the existence of water inevitably hydrolyzes the 1, 2-butylene oxide and isomers thereof to generate corresponding diol, the diol reacts with methanol to generate butanediol monomethyl ether, and the butanediol monomethyl ether continuously reacts with methanol to generate butanediol dimethyl ether. Taking 1, 2-epoxybutane as an example, 1, 2-epoxybutane is hydrolyzed to generate 1, 2-butanediol, 1, 2-butanediol reacts with impurity methanol to generate 2-methoxy-1-butanol, 1-methoxy-2-butanol, 2-methoxy-1-butanol and 1-methoxy-2-butanol, and the hydrolysis reaction continues to be carried out with time. If butanediol monomethyl ether and butanediol dimethyl ether in the extractant are not separated and removed, the butanediol dimethyl ether and the butanediol dimethyl ether can be continuously accumulated, so that the effective content of the circulating extractant is reduced, the extraction efficiency of the extractant is reduced, the energy consumption of a system is increased, and the purity of the epoxybutane is reduced.
Document US4402794 discloses a single extractive rectification separation of impurities such as water, methanol, acetone, methyl formate and the like contained in a crude 1, 2-butylene oxide solution using C7-C9 hydrocarbons, preferably n-octane, as extractant. The organic layer obtained after layering by the phase separator at the top of the extractive distillation tower is sent to a rectifying tower to distill and separate methanol, acetone and the like; feeding the material flow in the bottom of the extractive distillation tower into an extractive distillation tower; and discharging the tower bottom liquid of the extraction and rectification tower. The method reduces the accumulation of the extractant in the extractant by discharging part of the tower bottom liquid containing the extractant and the 1, 2-butanediol. Because the content of 1, 2-butanediol in partial material flow discharged from the tower bottom is low, a large amount of extractant needs to be discharged to ensure the purity of the extractant, and a large amount of extractant is lost.
Document US4772732 discloses a process for purifying butene oxide by using an anion exchange resin and an adsorbent. The anion exchange resin removes acid and dehydrogenation impurities, while the adsorbent removes water from impurities of butylene oxide. The purification steps may be carried out individually or in combination, depending on the impurity content, and the process may be carried out batchwise in a reactor or continuously in a column or column. The ion exchange resin selected is a sulfonated macroreticular anion exchange resin and the adsorbent is a molecular sieve. The method has high cost, troublesome adsorption and analysis process and low treatment capacity.
In conclusion, the washing method can reduce the content of glycol in the extractant, but the retention time required by liquid-liquid phase separation is long, the liquid-liquid extraction efficiency is low, the loss of the extractant is increased, meanwhile, the hydrolysis of the butylene oxide is increased, and the loss rate of the butylene oxide is increased; in addition, because the glycol has high boiling point and forms an azeotrope with the extractant, the separation of the extractant by distillation increases the equipment investment, the energy consumption is higher, and the economic benefit is low from the economic perspective; the adsorption and standing separation method has the problems of low efficiency and small scale; the extraction separation method has the problem of purification of an extracting agent.
The current situation of the prior art is that a butylene oxide purification method with low extractant loss, high purity, high butylene oxide yield and low energy consumption is still needed.
Disclosure of Invention
The present inventors have found, through studies based on the prior art, that at least one of the above-mentioned problems can be solved by forming a low temperature azeotrope with an extractant, butanediol monomethyl ether and butanediol dimethyl ether as impurities, and extracting the low temperature azeotrope from a side line liquid phase of a separation column using the azeotrope and the azeotropic type, and have accomplished the present invention.
In particular, the invention relates to a method for purifying epoxybutane. The method comprises the steps of separating a feed stream containing butylene oxide, an extractant and butanediol monomethyl ether and butanediol dimethyl ether in a separation column;
the separation column is operated under conditions sufficient for the extractant and butanediol monomethyl ether, butanediol dimethyl ether to form an azeotrope, and
collecting a material flow containing an extractant-butanediol monomethyl ether azeotrope and an extractant-butanediol dimethyl ether azeotrope from the side line of the separation tower.
According to one aspect of the invention, the conditions sufficient for the extractant and butanediol monomethyl ether, butanediol dimethyl ether to form an azeotrope comprise: the operation pressure at the tower top is 0.02-0.35 MPaG, preferably 0.02-0.20 MPaG; the operation temperature of the tower top is 69-118 ℃, and preferably 69-102 ℃.
According to one aspect of the invention, the number of theoretical plates of the separation column is 15 to 80, preferably 20 to 65, and more preferably 20 to 50.
According to one aspect of the invention, the weight ratio of the extractant to the butylene oxide in the feed stream is (2-20): 1, preferably (3-15): 1, more preferably (5-10): 1; the total content of the butanediol monomethyl ether and the butanediol dimethyl ether is 0.001-2.0% by weight, preferably 0.001-1.5% by weight, and more preferably 0.001-1.0% by weight.
According to one aspect of the invention, the feed stream is derived from an extracted product stream obtained by extractive distillation of a butene epoxidation reaction product.
According to one aspect of the invention, the side-stream of the separation column takes off the stream containing the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope at a position between 0.01N and 0.95N, preferably at a position between 0.05N and 0.85N.
According to one aspect of the invention, the flow rate of the material flow containing the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope, which is extracted from the side line of the separation tower, and the flow rate of butanediol monomethyl ether and butanediol dimethyl ether contained in the raw material flow are in a ratio of (1-10): 1, preferably (1-8): 1, and more preferably (1-4): 1.
According to one aspect of the invention, the separation column side is divided into at least two streams, a stream rich in the extractant-butanediol monomethyl ether azeotrope and a stream rich in the extractant-butanediol dimethyl ether azeotrope being withdrawn separately.
According to one aspect of the invention, the position of the material flow for extracting the extractant-butanediol dimethyl ether azeotrope is arranged at the upper part of the position of the material flow for extracting the extractant-butanediol monomethyl ether azeotrope.
According to one aspect of the invention, the side-line of the separation column produces a single stream containing the extractant butanediol monomethyl ether azeotrope and the extractant butanediol dimethyl ether azeotrope.
According to one aspect of the invention, the material flow containing the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope enters a phase separator, and a light phase material flow rich in the extractant and a heavy phase material flow rich in butanediol monomethyl ether and butanediol dimethyl ether are obtained after phase separation; the light phase material flow returns to the separation tower, and the heavy phase material flow is extracted.
According to one aspect of the invention, the material flow containing the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope is cooled to 30-60 ℃ and then enters the phase separator.
The invention has the beneficial effects that: according to the method, the extractant, the butanediol monomethyl ether and butanediol dimethyl ether heavy component impurities are utilized to form an azeotrope, and the azeotrope is extracted from the side line of the separation tower, so that the butanediol monomethyl ether and butanediol dimethyl ether impurities are discharged from the extractant circulating system, the circulating extractant is purified, the purity of the extractant is improved, the loss and energy consumption of the extractant are reduced, and the yield of the epoxybutane is improved. Compared with the scheme that the material flow part in the tower kettle of the separation tower is directly discharged, the purity of the extracting agent is improved by 0.1-14%, the loss of the extracting agent is 0.01-1%, the energy consumption is reduced by 1-16%, and the yield of the epoxy butane is improved by 0.5-5%.
Drawings
FIG. 1 is a schematic flow diagram of one embodiment of the present invention.
FIG. 2 is a schematic flow chart of another embodiment of the present invention.
FIG. 3 is a schematic flow chart of another embodiment of the present invention.
FIG. 4 is a schematic flow chart of a comparative example.
In the drawings, like parts are provided with like reference numerals. The drawings are not to scale.
Description of reference numerals:
1 feed stream
2 extractant stream
3 butylene oxide product stream
4 reboiler feed stream
6 side draw stream (second stream) rich in extractant-butanediol dimethyl ether azeotrope
7 side-draw stream (first stream) rich in extractant-butanediol monomethyl ether azeotrope
8 Material flow containing extractant-butanediol monomethyl ether azeotrope and extractant-butanediol dimethyl ether azeotrope
9 light phase stream rich in extractant
10 heavy phase stream rich in butanediol monomethyl ether and butanediol dimethyl ether
11 heavy ends contaminant stream
A separation tower
B reboiler
C cooler
D phase splitter
The invention is described in detail below with reference to the drawings, but it is to be noted that the scope of the invention is not limited thereto, but is defined by the appended claims.
All publications, patent applications, patents, and other references mentioned in this specification are herein incorporated by reference in their entirety. Unless defined otherwise, all technical and scientific terms used herein have the same meaning as commonly understood by one of ordinary skill in the art. In case of conflict, the present specification, including definitions, will control.
When the specification concludes with claims with the heading "known to those skilled in the art", "prior art", or the like, to derive materials, substances, methods, procedures, devices, or components, etc., it is intended that the subject matter derived from the heading encompass those conventionally used in the art at the time of filing this application, but also include those that are not currently in use, but would become known in the art to be suitable for a similar purpose.
In the context of the present specification, anything or things which are not mentioned, except where explicitly stated, are directly applicable to those known in the art without any changes. Moreover, any embodiment described herein may be freely combined with one or more other embodiments described herein, and the technical solutions or concepts resulting therefrom are considered part of the original disclosure or original disclosure of the invention, and should not be considered as new matters not disclosed or contemplated herein, unless a person skilled in the art would consider such a combination to be clearly unreasonable.
Unless otherwise expressly indicated, all percentages, parts, ratios, etc. mentioned in this specification are by weight unless otherwise not in accordance with the conventional knowledge of those skilled in the art.
In the case where no explicit indication is given, the number of theoretical plates mentioned in this specification is calculated from top to bottom, i.e. the overhead condenser is the first theoretical plate and the kettle reboiler is the last theoretical plate.
Reference to pressure within this specification refers to relative pressure unless explicitly indicated.
The feed used in the purification process of the invention is a stream comprising butylene oxide and an extractant. This stream is derived from the extract product stream obtained after extractive distillation of the olefin epoxidation reaction product in an extractive distillation column (not shown in the drawing). In the material flow, the weight ratio of the extracting agent to the epoxy butane is (2-20): 1, preferably (3-15): 1, more preferably (5-10): 1; the total content of the butanediol monomethyl ether and the butanediol dimethyl ether is 0.001-2.0% by weight, preferably 0.001-1.5% by weight, and more preferably 0.001-1.0% by weight. The butanediol monomethyl ether is generated by the reaction of hydrolysate glycol of butylene oxide and methanol, and the butanediol dimethyl ether is generated by the continuous reaction of the butanediol monomethyl ether and the methanol. The butylene oxide includes 1, 2-butylene oxide and isomers thereof such as 1, 4-butylene oxide, 2, 3-butylene oxide, and isobutylene oxide. Taking 1, 2-butylene oxide as an example, 1, 2-butylene oxide is hydrolyzed to generate 1, 2-butylene glycol, 1, 2-butylene glycol reacts with impurity methanol to generate 2-methoxy-1-butanol, 1-methoxy-2-butanol, 2-methoxy-1-butanol and 1-methoxy-2-butanol, and then the reaction with methanol is continued to generate 1, 2-butylene glycol dimethyl ether. Taking 1, 4-butylene oxide as an example, 1, 4-butylene oxide is hydrolyzed to generate 1, 4-butylene glycol, 1, 4-butylene glycol reacts with impurity methanol to generate 1-methoxy-4-butanol, and 1-methoxy-4-butanol continuously reacts with methanol to generate 1, 4-butylene glycol dimethyl ether. Taking 2, 3-epoxybutane as an example, 2, 3-epoxybutane is hydrolyzed to generate 2, 3-butanediol, 2, 3-butanediol reacts with impurity methanol to generate 2-methoxy-3-butanol, and 2-methoxy-3-butanol continuously reacts with methanol to generate 2, 3-butanediol dimethyl ether.
According to the invention, in figure 1, a material flow 1 containing butylene oxide, an extracting agent and impurities of butanediol monomethyl ether and butanediol dimethyl ether enters a separation tower A, a butylene oxide product material flow 3 is removed from the top of the separation tower, an extracting agent material flow 2 is removed from the bottom of the separation tower, and the removed extracting agent can be returned to a previous extraction rectifying tower (not shown in the figure of the invention) for recycling. The bottom of the separation tower A is provided with a reboiler B, the reboiler B feeds 4 tower bottoms into the reboiler B, a reboiler B discharge material flow 5 is obtained after heating, the discharge material flow 5 is fed back to the lower part of the separation tower A, and a side-draw material flow 7 containing an extractant-butanediol monomethyl ether azeotrope and an extractant-butanediol dimethyl ether azeotrope is drawn from the side of the separation tower A. Thereby, butanediol monomethyl ether and butanediol dimethyl ether as impurities are discharged from the system.
The use of extractive agents for the purification of butylene oxide is well known. Generally, C7-C20 straight-chain and branched-chain hydrocarbons and/or glycols are used as the extractant. The inventor researches and discovers that in an azeotrope formed by an extracting agent and impurities of butanediol monomethyl ether and butanediol dimethyl ether, the n-octane content is lowest and the advantage is greatest, 2-methylheptane is second and the advantage of isooctane is lowest, so that the invention selects C8 alkane as the extracting agent when the extracting agent is selected, preferably C8 alkane contains an isomer of methyl or C8 normal alkane as the extracting agent, and more preferably C8 normal alkane as the extracting agent.
The inventor researches and discovers that in an azeotropic composition formed by an extracting agent and impurities of butanediol monomethyl ether and butanediol dimethyl ether, the content of the impurities is increased along with the increase of pressure. That is, under the condition that the side-draw amount is the same, the higher the pressure of the separation tower is, the more butanediol monomethyl ether and butanediol dimethyl ether are produced as impurities. However, the higher the pressure, the higher the temperature at the top of the column, the higher the temperature of the butylene oxide is, the side reactions such as polymerization can occur, the yield of the butylene oxide is reduced, and the higher the temperature of the bottom of the column is, the higher the steam grade is required. Therefore, the operation pressure at the top of the tower is 0.02-0.35 MPaG, preferably 0.02-0.20 MPaG, the optimal extraction composition is the azeotropic composition corresponding to the operation pressure, otherwise, the amount of the extracting agent in the side extraction composition is increased, and the loss amount of the extracting agent in the side extraction composition is increased.
According to the invention, the side offtake of the separation column is located at a position between 0.01N and 0.95N, preferably between 0.05N and 0.85N. At this location, the azeotrope composition had the highest content of butanediol monomethyl ether and butanediol dimethyl ether, and the amount of butylene oxide carried over from the side draw stream was the least. The higher the concentration of the epoxybutane in the azeotrope composition, and the lower the concentrations of impurities butanediol monomethyl ether and butanediol dimethyl ether, the more the epoxybutane is taken out when the azeotrope is extracted, and the greater the loss is.
The side-stream azeotrope can be taken out in a single stream or in two streams, preferably in a single side stream.
FIG. 2 is an embodiment of the invention where the side azeotrope is split into at least two streams, the number of streams in the side stream being consistent with the number of impurity species. At least two side draws are: a first stream rich in extractant-butanediol monomethyl ether azeotrope, and a second stream rich in extractant-butanediol dimethyl ether azeotrope. The first stream comprises the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope, but is rich in the extractant-butanediol monomethyl ether azeotrope and is the highest in butanediol monomethyl ether concentration in the extractant-butanediol monomethyl ether azeotrope. The second stream comprises an extractant-butanediol monomethyl ether azeotrope and an extractant-butanediol dimethyl ether azeotrope, but is rich in the extractant-butanediol dimethyl ether azeotrope and is the highest concentration of butanediol dimethyl ether in the extractant-butanediol dimethyl ether azeotrope. The second stream withdrawal port is positioned above the first stream withdrawal port.
The density of the extractant such as n-octane is 0.690g/cm3(40 ℃ C.), the density of butanediol monomethyl ether is 1.25g/cm3(40 ℃), the density of butanediol dimethyl ether is 0.917g/cm3(25 ℃), the density difference between the extractant and the butanediol monomethyl ether and butanediol dimethyl ether is large, and the gravity settling separation is easy to adopt. Fig. 3 is a preferred embodiment of the present invention. Cooling the material flow 8 containing the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope by a cooler C, preferably cooling to 30-60 ℃, then feeding the material flow into a phase separator D, and performing phase separation to obtain a light phase material flow rich in the extractant and a heavy phase material flow rich in butanediol monomethyl ether and butanediol dimethyl ether; the light phase material flow returns to the separation tower, and the heavy phase material flow is extracted. The light phase rich in the extractant is returned and separated after the side line extraction is cooled and phase-separatedThe technical scheme of the tower can greatly improve the purity of the extracting agent and reduce the loss of the extracting agent. For a better separation of the oxygenate impurities of butanediol monomethyl ether, butanediol dimethyl ether and the extractant, water or medium-pressure steam can be added to the phase separator, since the oxygenate impurities are soluble in water, whereas the extractant hydrocarbons are practically insoluble in water.
Fig. 4 is prior art, a material flow 1 containing butylene oxide, an extracting agent and impurities enters a separation tower A, a butylene oxide product material flow 3 is moved out from the top of the separation tower A, an extracting agent material flow 2 is moved out from the bottom of the separation tower A, a reboiler B is arranged at the bottom of the separation tower A, a tower bottom liquid is sent into the reboiler B by a reboiler B feeding material flow 4, a reboiler B discharging material flow 5 is obtained after heating, the discharging material flow 5 is sent into the lower part of the separation tower A, a heavy component impurity material flow 11 is separated from the extracting agent material flow 2, and therefore impurities of butanediol monomethyl ether and butanediol dimethyl ether are discharged out of the system. A greater amount of extractant is lost due to the reduction of impurity build-up in the extractant by the discharge of a portion of the bottoms stream.
The invention is further illustrated by the following specific embodiments.
Detailed Description
[ example 1 ]
According to the process flow shown in FIG. 1, the extraction agent is n-octane, the ratio of the extraction agent to 1, 2-butylene oxide is 5:1, the number of theoretical plates in the separation column is 20, and the side line of the separation column is located at the 7 th theoretical plate in the material flow containing 1, 2-butylene oxide, the extraction agent and impurities of 2-methoxy-1-butanol, 1-methoxy-2-butanol and 1, 2-butylene glycol dimethyl ether. The operating pressure of the separation tower is 0.02MPaG, the temperature of the top of the separation tower is 69 ℃, the side line extraction temperature is 91 ℃, the content of impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and 1, 2-butanediol dimethyl ether is 18.30 wt%, and the side line impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and 1, 2-butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 1, the purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.95%, the purity of the extractant at the bottom of the separation tower is 99.71%, and the loss of the extractant is 0.286%.
According to the process flow shown in figure 2, the side-draw position respectively selects the maximum content of impurities of 2-methoxy-1-butanol, 1-methoxy-2-butanol and 1, 2-butanediol dimethyl ether. The number of the side-drawn material flow is consistent with the number of the impurity types. In the raw materials of the invention, 3 impurities exist, so the side draw is 3 strands.
The 17 th theoretical plate extracts 2-methoxy-1-butanol as an impurity, wherein the side extraction temperature is 129 ℃, the content of the 2-methoxy-1-butanol as the impurity is 0.28 wt%, the content of the 1-methoxy-2-butanol as the impurity is 9.53 wt%, and the content of the dimethyl ether of butanediol is 1.46 wt%.
The 15 th theoretical plate extracts 1-methoxy-2-butanol as an impurity, wherein the side extraction temperature is 127 ℃, the content of the 1-methoxy-2-butanol as the impurity is 15.71 wt%, the content of the 2-methoxy-1-butanol as the impurity is 0.12 wt%, and the content of the dimethyl ether of butanediol is 4.60 wt%.
The 7 th plate extracts the impurity butanediol dimethyl ether, wherein the side-line extraction temperature is 74 ℃, the butanediol dimethyl ether content is 10.45 wt%, the impurity 1-methoxyl-2-butanol content is 0.02 wt%, and the impurity 2-methoxyl-1-butanol content is 1.3 ppm.
The total amount of the impurities extracted in the three streams is 14.20 wt%.
According to the process flow shown in fig. 2, the purity of the 1, 2-butylene oxide product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.90%, the purity of the extractant at the bottom of the separation tower is 99.78%, and the loss of the extractant is 0.281%.
Under the condition that the total amount of the side offtake is the same, 4.10% more impurities are extracted according to the process flow shown in the figure 1 than the process flow shown in the figure 2, and because the side offtake amount of the 1, 2-epoxybutane is increased in the process flow shown in the figure 2, the recovery rate of the 1, 2-epoxybutane is reduced, and the loss rate of the extracting agent is slightly reduced.
[ example 2 ]
According to the process flow shown in figure 1, the extracting agent is n-octane, the ratio of the extracting agent to the 1, 2-butylene oxide is 5:1 in weight percentage in the material flow containing the 1, 2-butylene oxide, the extracting agent and impurities of the 2-methoxy-1-butanol, the 1-methoxy-2-butanol and the butanediol dimethyl ether, the theoretical plate number of the separation tower is 20, and the 7 th theoretical plate is extracted from the side line of the separation tower. The operating pressure of the separation tower is 0.06MPaG, the temperature of the top of the separation tower is 79 ℃, the temperature of the side line extraction is 101 ℃, the contents of impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are 18.58 wt%, and the side line impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 1, the purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.94%, the purity of the extractant at the bottom of the separation tower is 99.73%, and the loss of the extractant is 0.283%.
[ example 3 ]
According to the process flow shown in figure 1, the extracting agent is n-octane, the ratio of the extracting agent to the 1, 2-butylene oxide is 5:1 in weight percentage in the material flow containing the 1, 2-butylene oxide, the extracting agent and impurities of the 2-methoxy-1-butanol, the 1-methoxy-2-butanol and the butanediol dimethyl ether, the theoretical plate number of the separation tower is 20, and the 7 th theoretical plate is extracted from the side line of the separation tower. The operating pressure of the separation tower is 0.10MPaG, the tower top temperature is 86 ℃, the side line extraction temperature is 109 ℃, the contents of impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are 18.82 wt%, and the side line impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 1, the purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.93%, the purity of the extractant at the bottom of the separation tower is 99.76%, and the loss of the extractant is 0.274%.
[ example 4 ]
According to the process flow shown in figure 1, the extracting agent is n-octane, the ratio of the extracting agent to the 1, 2-butylene oxide is 5:1 in weight percentage in the material flow containing the 1, 2-butylene oxide, the extracting agent and impurities of the 2-methoxy-1-butanol, the 1-methoxy-2-butanol and the butanediol dimethyl ether, the theoretical plate number of the separation tower is 20, and the 7 th theoretical plate is extracted from the side line of the separation tower. The operating pressure of the separation tower is 0.14MPaG, the tower top temperature is 93 ℃, the side line extraction temperature is 116 ℃, the contents of impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are 19.04 wt%, and the side line impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 1, the purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.92%, the purity of the extractant at the bottom of the separation tower is 99.78%, and the loss of the extractant is 0.271%.
[ example 5 ]
According to the process flow shown in figure 1, the extracting agent is n-octane, the ratio of the extracting agent to the 1, 2-butylene oxide is 5:1 in weight percentage in the material flow containing the 1, 2-butylene oxide, the extracting agent and impurities of the 2-methoxy-1-butanol, the 1-methoxy-2-butanol and the butanediol dimethyl ether, the theoretical plate number of the separation tower is 20, and the 7 th theoretical plate is extracted from the side line of the separation tower. The operating pressure of the separation tower is 0.17MPaG, the tower top temperature is 97 ℃, the side line extraction temperature is 121 ℃, the contents of 19.19 wt% of impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted, and the side line impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 1, the purity of the 1, 2-butylene oxide product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.90%, the purity of the extractant at the bottom of the separation tower is 99.81%, and the loss of the extractant is 0.265%.
[ example 6 ]
According to the process flow shown in figure 1, the extracting agent is n-octane, the ratio of the extracting agent to the 1, 2-butylene oxide is 5:1 in weight percentage in the material flow containing the 1, 2-butylene oxide, the extracting agent and impurities of the 2-methoxy-1-butanol, the 1-methoxy-2-butanol and the butanediol dimethyl ether, the theoretical plate number of the separation tower is 20, and the 7 th theoretical plate is extracted from the side line of the separation tower. The operating pressure of the separation tower is 0.20MPaG, the tower top temperature is 102 ℃, the side line extraction temperature is 126 ℃, the contents of impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are 19.35 wt%, and the side line impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 1, the purity of the 1, 2-butylene oxide product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.89%, the purity of the extractant at the bottom of the separation tower is 99.84%, and the loss of the extractant is 0.260%.
[ example 7 ]
According to the process flow shown in figure 1, the extracting agent is n-octane, the ratio of the extracting agent to the 1, 2-butylene oxide is 6:1 in weight percentage in the material flow containing the 1, 2-butylene oxide, the extracting agent and impurities of the 2-methoxy-1-butanol, the 1-methoxy-2-butanol and the butanediol dimethyl ether, the theoretical plate number of the separation tower is 30, and the side line of the separation tower is drawn on the 12 th theoretical plate. The operating pressure of the separation tower is 0.02MPaG, the temperature of the top of the separation tower is 69 ℃, the temperature of the side line extraction is 91 ℃, the contents of impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are 18.88 wt%, and the side line impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 1, the purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.96%, the recovery rate is 99.96%, the purity of the extractant at the bottom of the separation tower is 99.89%, and the loss of the extractant is 0.239%.
[ example 8 ]
According to the process flow shown in figure 1, the extracting agent is n-octane, the ratio of the extracting agent to the 1, 2-butylene oxide is 7:1 in weight percent in the material flow containing the 1, 2-butylene oxide, the extracting agent and impurities of the 2-methoxy-1-butanol, the 1-methoxy-2-butanol and the butanediol dimethyl ether, the theoretical plate number of the separation tower is 40, and the 15 th theoretical plate is extracted from the side line of the separation tower. The operating pressure of the separation tower is 0.02MPaG, the temperature of the top of the separation tower is 69 ℃, the temperature of the side line extraction is 91 ℃, the contents of impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are 18.93 wt%, and the side line impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 1, the purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.97%, the recovery rate is 99.97%, the purity of the extractant at the bottom of the separation tower is 99.92%, and the loss of the extractant is 0.205%.
[ example 9 ]
According to the process flow shown in figure 1, the extracting agent is n-octane, the ratio of the extracting agent to the 1, 2-butylene oxide is 10:1 in weight percentage in the material flow containing the 1, 2-butylene oxide, the extracting agent and impurities of the 2-methoxy-1-butanol, the 1-methoxy-2-butanol and the butanediol dimethyl ether, the theoretical plate number of the separation tower is 50, and the side line of the separation tower is used for collecting the 19 th theoretical plate. The operating pressure of the separation tower is 0.02MPaG, the temperature of the top of the separation tower is 69 ℃, the temperature of the side line extraction is 91 ℃, the contents of impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are 18.98 wt%, and the side line impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 1, the purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.97%, the recovery rate is 99.97%, the purity of the extractant at the bottom of the separation tower is 99.95%, and the loss of the extractant is 0.178%.
[ example 10 ]
According to the process flow shown in figure 1, the extracting agent is n-octane, the ratio of the extracting agent to the 1, 2-butylene oxide is 5:1 in weight percentage in the material flow containing the 1, 2-butylene oxide, the extracting agent and impurities of the 2-methoxy-1-butanol, the 1-methoxy-2-butanol and the butanediol dimethyl ether, the theoretical plate number of the separation tower is 20, and the side line of the separation tower is used for collecting the 6 th theoretical plate. The operating pressure of the separation tower is 0.02MPaG, the temperature of the top of the separation tower is 69 ℃, the temperature of the side line extraction is 89 ℃, the contents of impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are 17.32 wt%, and the side line impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 1, the purity of the 1, 2-butylene oxide product obtained at the top of the separation tower is 99.95%, the recovery rate is 99.94%, the purity of the extractant at the bottom of the separation tower is 99.69%, and the loss of the extractant is 0.298%.
[ example 11 ]
According to the process flow shown in fig. 3, the extracting agent is n-octane, the ratio of the extracting agent to the 1, 2-butylene oxide is 6:1 in the material flow containing the 1, 2-butylene oxide, the extracting agent and impurities of the 2-methoxy-1-butanol, the 1-methoxy-2-butanol and the butanediol dimethyl ether according to the weight percentage, the theoretical plate number of the separation tower is 30, and the side line of the separation tower is drawn on the 12 th theoretical plate.
The side-draw flow is 1.5:1 of the impurity flow contained in the feed flow, the operating pressure of the separation tower is 0.025MPaG, the tower top temperature is 71 ℃, the side-draw temperature is 93 ℃, the contents of impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are 18.96 wt%, and the side-draw impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 3, the purity of the 1, 2-butylene oxide product obtained at the top of the separation tower is 99.96%, the recovery rate is 99.96%, the purity of the extractant at the bottom of the separation tower is 99.93%, and the loss of the extractant is 0.197%.
[ example 12 ]
According to the process flow shown in FIG. 3, the extractant is n-octane, the ratio of the extractant to 1, 2-butylene oxide is 7:1 in weight percent in the material flow containing 1, 2-butylene oxide, extractant and impurities of 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether, the theoretical plate number of the separation tower is 40, and the 15 th theoretical plate is extracted from the side line of the separation tower.
The side draw flow is 2:1 of the impurity flow contained in the feed flow, the operating pressure of the separation tower is 0.05MPaG, the tower top temperature is 77 ℃, the side draw temperature is 99 ℃, the contents of impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are 18.49 wt%, and the side impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 3, the purity of the 1, 2-butylene oxide product obtained at the top of the separation tower is 99.96%, the recovery rate is 99.95%, the purity of the extractant at the bottom of the separation tower is 99.92%, and the loss of the extractant is 0.211%.
[ example 13 ]
According to the process flow shown in FIG. 3, the extractant is n-octane, the ratio of the extractant to 1, 2-butylene oxide is 8:1 in weight percent in the material flow containing 1, 2-butylene oxide, extractant and impurities of 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether, the theoretical plate number of the separation tower is 20, and the 7 th theoretical plate is extracted from the side line of the separation tower.
The side-draw flow is 2.5:1 of the impurity flow contained in the feed flow, the operating pressure of the separation tower is 0.11MPaG, the tower top temperature is 88 ℃, the side-draw temperature is 110 ℃, the contents of the impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are 18.11 wt%, and the side-draw impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 3, the purity of the 1, 2-butylene oxide product obtained at the top of the separation tower is 99.96%, the recovery rate is 99.93%, the purity of the extractant at the bottom of the separation tower is 99.90%, and the loss of the extractant is 0.231%.
[ example 14 ]
According to the process flow shown in FIG. 3, the extractant is n-octane, the ratio of the extractant to 1, 2-butylene oxide is 9:1 in weight percent in the material flow containing 1, 2-butylene oxide, extractant and impurities of 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether, the theoretical plate number of the separation tower is 20, and the side line of the separation tower is located at the 6 th theoretical plate.
The side-draw flow is 3:1 of the impurity flow contained in the feed flow, the operating pressure of the separation tower is 0.15MPaG, the tower top temperature is 94 ℃, the side-draw temperature is 119 ℃, the contents of impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are 17.76 wt%, and the side-draw impurities 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are enriched and extracted.
According to the process flow shown in fig. 3, the purity of the 1, 2-butylene oxide product obtained at the top of the separation tower is 99.96%, the recovery rate is 99.92%, the purity of the extractant at the bottom of the separation tower is 99.88%, and the loss of the extractant is 0.245%.
[ example 15 ]
According to the process flow shown in FIG. 3, the extractant is n-octane, the ratio of the extractant to 1, 2-butylene oxide is 10:1 in weight percent in the material flow containing 1, 2-butylene oxide, extractant and impurities of 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether, the theoretical plate number of the separation tower is 50, and the 17 th theoretical plate is extracted from the side line of the separation tower.
The side-draw flow is 4:1 of the impurity flow contained in the feed flow, the operating pressure of the separation tower is 0.20MPaG, the tower top temperature is 101 ℃, the side-draw temperature is 127 ℃, the contents of impurities, namely 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether, are 17.34 wt%, and the side-draw impurities, namely 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether, are enriched and extracted.
According to the process flow shown in fig. 3, the purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.96%, the recovery rate is 99.90%, the purity of the extractant at the bottom of the separation tower is 99.85%, and the loss of the extractant is 0.253%.
[ COMPARATIVE EXAMPLE 1 ]
According to the process flow diagram shown in FIG. 4, the extractant is n-octane, the ratio of the extractant to 1, 2-butylene oxide is 5:1 in weight percent in the material flow containing 1, 2-butylene oxide, the extractant and impurities of 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether, the theoretical plate number of the separation tower is 20, and the impurity material flow is extracted from the bottom of the separation tower. The operating pressure of the separation tower is 0.02MPaG, the temperature is 69 ℃, the temperature of the impurity material flow extracted from the tower bottom is 137 ℃, the content of the impurities of 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether is 0.398 wt%, and the impurities of 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are extracted.
According to the process flow shown in fig. 1, the purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.99%, the recovery rate is 99.99%, the purity of the extractant at the bottom of the separation tower is 99.52%, and the loss of the extractant is 0.651%.
[ COMPARATIVE EXAMPLE 2 ]
According to the process flow diagram shown in FIG. 4, the extractant is 2-methylheptane, the ratio of the extractant to 1, 2-butylene oxide is 5:1 in terms of weight percentage in the material flow containing 1, 2-butylene oxide, the extractant and impurities of 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether, the theoretical plate number of the separation tower is 20, and the impurity material flow is extracted from the bottom of the separation tower. The operating pressure of the separation tower is 0.02MPaG, the temperature is 69 ℃, the temperature of an impurity material flow extracted from a tower bottom is 129 ℃, the content of impurities of 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether is 0.398 wt%, and the impurities of 2-methoxy-1-butanol, 1-methoxy-2-butanol and butanediol dimethyl ether are extracted.
According to the process flow shown in fig. 1, the purity of the 1, 2-epoxybutane product obtained at the top of the separation tower is 99.99%, the recovery rate is 99.99%, the purity of the extractant at the bottom of the separation tower is 99.52%, and the loss of the extractant is 0.651%.
Claims (15)
1. A method for purifying butylene oxide comprises the steps of separating a feed stream containing butylene oxide, an extracting agent, butanediol monomethyl ether and butanediol dimethyl ether in a separation tower;
the separation column is operated under conditions sufficient for the extractant and butanediol monomethyl ether, butanediol dimethyl ether to form an azeotrope, and
collecting a material flow containing an extractant-butanediol monomethyl ether azeotrope and an extractant-butanediol dimethyl ether azeotrope from the side line of the separation tower;
the extractant is selected from C8At least one of an alkane;
the conditions sufficient for the extractant and butanediol monomethyl ether, butanediol dimethyl ether to form an azeotrope include: the operation pressure at the top of the tower is 0.02-0.20 MPaG, and the operation temperature at the top of the tower is 69-102 ℃;
the position of the material flow which is extracted from the side line of the separation tower and contains the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope is positioned between 0.05N and 0.85N;
the method further comprises the following steps: the material flow containing the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope enters a phase separator, and a light phase material flow rich in the extractant and a heavy phase material flow rich in butanediol monomethyl ether and butanediol dimethyl ether are obtained after phase separation; the light phase material flow returns to the separation tower, and the heavy phase material flow is extracted.
2. The method for purifying butylene oxide according to claim 1, wherein the number of theoretical plates of the separation column is 15 to 80.
3. The method for purifying butylene oxide according to claim 2, wherein the number of theoretical plates of the separation column is 20 to 65.
4. The method for purifying butylene oxide according to claim 3, wherein the number of theoretical plates of the separation column is 20 to 50.
5. The method for purifying butylene oxide according to claim 1, wherein the weight ratio of the extractant to butylene oxide in the feed stream is (2-20): 1; the total content of the butanediol monomethyl ether and the butanediol dimethyl ether is 0.001-2.0% by weight.
6. The method for purifying butylene oxide according to claim 5, wherein the weight ratio of the extractant to butylene oxide in the feed stream is (3-15): 1; the total content of the butanediol monomethyl ether and the butanediol dimethyl ether is 0.001-1.5% by weight.
7. The method for purifying butylene oxide according to claim 6, wherein the weight ratio of the extractant to butylene oxide in the feed stream is (5-10): 1; the total content of the butanediol monomethyl ether and the butanediol dimethyl ether is 0.001-1.0% by weight.
8. The process for purifying butylene oxide as recited in claim 1, wherein the feed stream is derived from an extract product stream obtained by extractive distillation of a product of the epoxidation of butene.
9. The method for purifying the butylene oxide according to claim 1, wherein the ratio of the flow rate of the material flow containing the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope, which is collected from the side line of the separation tower, to the flow rate of the butanediol monomethyl ether and butanediol dimethyl ether contained in the raw material flow is (1-10): 1.
10. The method for purifying the butylene oxide according to claim 9, wherein the ratio of the flow rate of the material flow containing the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope, which is collected from the side line of the separation tower, to the flow rate of the butanediol monomethyl ether and butanediol dimethyl ether contained in the raw material flow is (1-8): 1.
11. The method for purifying butylene oxide according to claim 10, wherein the ratio of the flow rate of the stream containing the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope, which is collected from the side line of the separation column, to the flow rate of butanediol monomethyl ether and butanediol dimethyl ether contained in the raw material stream is (1-4): 1.
12. The process for purifying butylene oxide as claimed in claim 1, wherein the separation column side is divided into at least two streams, and a stream rich in the extractant-butanediol monomethyl ether azeotrope and a stream rich in the extractant-butanediol dimethyl ether azeotrope are separately withdrawn.
13. The process for purifying butylene oxide as claimed in claim 12, wherein the position of the stream from which the extractant-butanediol dimethyl ether azeotrope is extracted is located above the position of the stream from which the extractant-butanediol monomethyl ether azeotrope is extracted.
14. The process for purifying butylene oxide according to claim 1, wherein a single stream containing the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope is withdrawn from the side of the separation column.
15. The method for purifying butylene oxide according to claim 14, wherein the stream containing the extractant-butanediol monomethyl ether azeotrope and the extractant-butanediol dimethyl ether azeotrope is cooled to 30-60 ℃ and then enters the phase separator.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| CN201711241023 | 2017-11-30 | ||
| CN2017112410231 | 2017-11-30 |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| CN109851581A CN109851581A (en) | 2019-06-07 |
| CN109851581B true CN109851581B (en) | 2021-06-18 |
Family
ID=66889559
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CN201810153545.4A Active CN109851581B (en) | 2017-11-30 | 2018-02-22 | Method for purifying butylene oxide |
Country Status (1)
| Country | Link |
|---|---|
| CN (1) | CN109851581B (en) |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN112851601B (en) * | 2019-11-27 | 2022-11-22 | 北京诺维新材科技有限公司 | Method for purifying alkylene oxide |
Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US4402794A (en) * | 1982-05-24 | 1983-09-06 | Atlantic Richfield Company | Purification of butylene oxides by extractive distillation with selected extractive distillation solvents |
| JPS5924982B2 (en) * | 1979-09-26 | 1984-06-13 | 昭和電工株式会社 | Purification method of butylene oxide |
| US5529667A (en) * | 1994-12-01 | 1996-06-25 | Hoechst Celanese Corporation | Process for recovering ethylene oxide |
| CN1633424A (en) * | 2002-02-15 | 2005-06-29 | 住友化学工业株式会社 | Method of purifying propylene oxide |
| CN1678600A (en) * | 2002-07-23 | 2005-10-05 | 巴斯福股份公司 | Method for the continuous purification by distillation of 1,2-propylene glycol that accumulates during the synthesis of propylene rpoxide without coupling products |
| CN101006067A (en) * | 2004-06-23 | 2007-07-25 | 住友化学株式会社 | Method of purifying propylene oxide |
| CN104109137A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Epoxypropane purifying method |
-
2018
- 2018-02-22 CN CN201810153545.4A patent/CN109851581B/en active Active
Patent Citations (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5924982B2 (en) * | 1979-09-26 | 1984-06-13 | 昭和電工株式会社 | Purification method of butylene oxide |
| US4402794A (en) * | 1982-05-24 | 1983-09-06 | Atlantic Richfield Company | Purification of butylene oxides by extractive distillation with selected extractive distillation solvents |
| US5529667A (en) * | 1994-12-01 | 1996-06-25 | Hoechst Celanese Corporation | Process for recovering ethylene oxide |
| CN1633424A (en) * | 2002-02-15 | 2005-06-29 | 住友化学工业株式会社 | Method of purifying propylene oxide |
| CN1678600A (en) * | 2002-07-23 | 2005-10-05 | 巴斯福股份公司 | Method for the continuous purification by distillation of 1,2-propylene glycol that accumulates during the synthesis of propylene rpoxide without coupling products |
| CN101006067A (en) * | 2004-06-23 | 2007-07-25 | 住友化学株式会社 | Method of purifying propylene oxide |
| CN104109137A (en) * | 2013-04-16 | 2014-10-22 | 中国石油化工股份有限公司 | Epoxypropane purifying method |
Also Published As
| Publication number | Publication date |
|---|---|
| CN109851581A (en) | 2019-06-07 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN109851586B (en) | Process for purifying propylene oxide | |
| CN109851576B (en) | Method and apparatus for purifying butylene oxide | |
| CN107915612B (en) | Method for preparing purified MIBK from industrial byproduct waste liquid acetone | |
| CN109851581B (en) | Method for purifying butylene oxide | |
| CN109851583B (en) | Alkylene oxide purification process | |
| EP3719008B1 (en) | Alkylene oxide production method and production system | |
| CN109851589B (en) | Propylene oxide purification method and purification apparatus | |
| CN107915615B (en) | Method for preparing purified MIBK from industrial byproduct waste liquid acetone | |
| CN109851577B (en) | Method for purifying butylene oxide | |
| CN105085165A (en) | Ethylene glycol and diethylene glycol separation method | |
| CN109851591B (en) | Method and apparatus for purifying alkylene oxide | |
| CN109851588B (en) | Method for purifying propylene oxide | |
| CN109851580A (en) | The purification process of epoxy butane | |
| CN109851585B (en) | Method for purifying butylene oxide | |
| CN109851587B (en) | Method for producing butylene oxide | |
| CN109851584B (en) | Method and apparatus for purifying alkylene oxide | |
| KR102458887B1 (en) | Method and system for production of alkylene oxide | |
| CN109851574B (en) | Method for producing propylene oxide | |
| CN113651778B (en) | Extraction agent pretreatment and replenishment method | |
| CN109851590A (en) | The purification process of propylene oxide |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| PB01 | Publication | ||
| PB01 | Publication | ||
| SE01 | Entry into force of request for substantive examination | ||
| SE01 | Entry into force of request for substantive examination | ||
| GR01 | Patent grant | ||
| GR01 | Patent grant |